EP0002880A2 - Régénération d'une solution absorbante - Google Patents

Régénération d'une solution absorbante Download PDF

Info

Publication number
EP0002880A2
EP0002880A2 EP78300471A EP78300471A EP0002880A2 EP 0002880 A2 EP0002880 A2 EP 0002880A2 EP 78300471 A EP78300471 A EP 78300471A EP 78300471 A EP78300471 A EP 78300471A EP 0002880 A2 EP0002880 A2 EP 0002880A2
Authority
EP
European Patent Office
Prior art keywords
sulphuric acid
thiosulphate
liquor
sulphate
acid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP78300471A
Other languages
German (de)
English (en)
Other versions
EP0002880A3 (en
EP0002880B1 (fr
Inventor
Frederick Farrington
Peter Spence Clough
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
British Gas PLC
Original Assignee
British Gas Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by British Gas Corp filed Critical British Gas Corp
Publication of EP0002880A2 publication Critical patent/EP0002880A2/fr
Publication of EP0002880A3 publication Critical patent/EP0002880A3/xx
Application granted granted Critical
Publication of EP0002880B1 publication Critical patent/EP0002880B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
    • C10G17/08—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acid-forming oxides
    • C10G17/085—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acid-forming oxides with oleum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/05—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by wet processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
    • C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
    • C10G17/04—Liquid-liquid treatment forming two immiscible phases
    • C10G17/06—Liquid-liquid treatment forming two immiscible phases using acids derived from sulfur or acid sludge thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • C10K1/128—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing organic oxygen transferring compounds, e.g. sulfoxides

Definitions

  • Thia invention relates to the treatment of aqueous effluents derived from wash liquors employed for the purification of gases and hydrocarbon liquids, by the removal of undesirable contaminants from such effluents. More particularly the invention relates to the removal of solubilised sulphur compounds from wash liquors employed for the removal of hydrogen sulphide from gases and hydrocarbon liquids.
  • the reagents may be redox systems whereby the hydrogen sulphide is solvated and oxidised to elemental sulphur with the concomitant reduction of the reagent.
  • the reagent may be reoxidised and thus regenerated for further use.
  • One such process for H 2 S removal using a redox system is known as the Stretford Process and is described in our UK Patent Specification No. 948270 wherein the redox system is typically a mixture of anthraquinone disulphonic acid salts and alkali metal vanadates.
  • the reagent system of Stretford Process is reoxidised and regenerated by air-blowing through the reduced liquor.
  • the air-blowing is also employed to remove elemental sulphur from the liquor which is formed during reduction of the reagent.
  • the presence of air and elemental sulphur causes some of the elemental sulphur to be solubilised in the form of sulphoxy compounds such as sulphate and thiosulphate. Solubilisation is also believed to occur at other times during the progress of the Stretford Process cycle.
  • the present invention proposes a process for destroying thiosulphates by reaction with sulphuric acid with substantially no sulphur dioxide production and under conditions which avoid the economical burdens proposed by the prior art processes.
  • a process for the conversion of water soluble thiosulphates to the corresponding sulphates wherein an aqueous solution containing said thiosulphates is fed to a reaction vessel, reacted with concentrated sulphuric acid and the reaction product comprising a sulphate is removed from the reaction vessel, the improvement consisting in effecting said reaction at about ambient pressure and at a temperature of from about 70 C to about 100 o C and wherein the sulphuric acid is sparged into the lower and of the vessel containing said aqueous solution.
  • the sulphuric acid with the liquor at the base of the reaction vessel.
  • This may be achieved by either pumping the acid directly into the bottom of the tank or by introducing the acid from the top directly through a dip tube terminating near the bottom of the vessel.
  • the contents of the reaction vessel are continuously agitated, e.g. by stirring.
  • reaction I Since the acid is introduced below the main mass of thiosulphate liquor is the reaction vessel, the sulphur dioxide produced in reaction I reacts with thoisulphate Viz thereby giving an overall reaction.
  • the process of the invention is particularly advantageous for destroying thiosulphates present in Stretford Liquors.
  • the presence of vanadium, inherently present in Stretford Liquors is also believed to have a catalytic effect in reducing sulphur dioxide formation.
  • the concentration of sulphuric acid in total liquor will vary depending upon the temperature at which it is desired to operate the process of the invention.
  • the acid concentration will therefore range from 0.3 to 1.0 gm mole for every gram mole of thiosulphate.
  • the temperature at which the process is carried out will vary from 70°C to 100°C, and preferably will be from about 85°C to 95°C.
  • the acid strength may vary from above 50% w/w to the most concentrated form available including oleum. However, it is preferred to employ from above 50% to 98% w/w H 2 SO 4 .
  • the process of the present invention may be carried out at any thiosulphate loading up to the solubility point of the thiosulphate, the solution undergoing reaction having regard to the temperature at which redox wash liquor normally works.
  • a typical Stretford liquor works at about 40°C, at which temperature the solubility of sodium thiosulphate is about 300 gm/litre.
  • the Stretford effluent may contain other solubilised sulphoxy compounds. Thus, it is not possible to achieve the theoretical 100% saturation loading of thiosulphate.
  • a Stretford Liquor at 40°C may be regarded as nearly saturated with sulphoxy compounds when it contains 120 gm/litre Na 2 S 2 O 3 and 100 gm/litre Na 2 SO 4 .
  • the invention is carried out at the highest loading consistent with maintaining solubility of all the solubilised sulphoxy compounds. It should be emphasised that the relationship of sulphoxy compound loading with temperature is considered for the working temperature of the wash liquor and not necessarily the temperature at which the acification is effected. Thus for acidification reaction which is carried out at temperatures above 70°C one still has to consider the sulphoxy dompound loading at, say, 40 C.
  • the sulphate present in the reaction product may be removed by conventional techniques for lowering its solubility in solutions.
  • the sulphate - containing solution may be cooled to induce crystallisation or the liquor may be heated to evaporate water.
  • the latter technique may be especially useful since the process system already contains appreciable amounts of useful heat.
  • the liquor contains other compounds, e.g. the redox components, the water should not be evaporated off to such a degree whereby the other solution components also come out of solution.
  • the sulphate may be rendered insoluble by a precipitation technique such as by the addition of a barium salt or by addition of an organic precipitant such as a lower alkanol, e.g. methenol
  • Sodium sulphate is a marketable commodity provided it can be produced in pure fom.
  • One of the disadvantages of removing sulphate directly from the acidification liquor is that the sulphate crystals are likely to be contaminated with elemental sulphur, which is also produced in the acidification process of this invention.
  • solubility lowering techniques may be applied to the acidification effluent, or preferably, to a separated side stream.
  • This process comprises contacting said gas or non-polar liquid with an aqueous alkaline wash liquor comprising a salt of an anthraquinone disulphuric acid or derivative thereof, and a compound of vanadium, contacting said liquor, after contact with said gas or liquid, with an oxygen containing gas, taking a first portion of said oxygenated liquor, acidifying said portion as described aforesaid, returning said acidified liquor to the remainder of the oxygenated liquor, taking a second portion of said mixed oxygenated and acidified liquor, removing elemental sulphur from said second portion and subjecting said elemental sulphur fee second portion to a solubility lowering technique to induce crystallisation of sodium sulphate,removing said sodium sulphate and returning said second portion, now free of elemental sulphur and sodium sulphate, to the remainder of said oxygenated liquor.
  • an aqueous alkaline wash liquor comprising a salt of an anthraquinone disulphuric acid or derivative thereof, and a compound of vana
  • the process of the present invention may be employed to increase the overall efficiency of the Stretford Process.
  • the main purification process may be carried out as described in our UK Patent Specification No. 948270 as well as according to our earlier UK Patent Specification Nos. 971233 and 878251 and US Patent Specification Nos. 2997439 and 3035889, all of which are incorporated herein by reference.
  • the aqueous alkaline solution may contain approximately 0.5% by weight of any of the isomerio anthraquinone disulphonic acids (which of course will be present in the form of their salts), and may be initially made alkaline by adding ammonia or an alkali metal carbonate or bicarbonate or other base. It has a pH above 7, the preferred value being from 8.5 to 9.5.
  • the compound of a metal having at least two valency states may be an ortho-, meta-, or pyrovanadate of ammonia vanadate or sodium orthovanadate. Which ever salt is initially added, it would appear that a meta-vanadate is formed in a solution having a pH of about 9. It is preferably added in such quantity as to give a solution of concentration M/1000 to M/20, although concentrations outside this range may be used.
  • metal compounds which may be used in addition to the vanadates are salts or iron, copper maganese, chromium, nickel and cobalt, for example ferrous sulphate or ferric chloride.
  • Such salts may be used in concentrations of M/1000 to M/100.
  • a chelating or sequestering agent for the vanadate examples include soluble tartrate such as sodium potassium tartrate or tartaric acid or ethylene diamine retraacetic acid (referred to hereinafter as EDTA), or citric acid or soluble citrates, present in sufficient quantity to complex at least a portion of the vanadate, in order to maintain the solubility of the vanadate in the presence of hydrosulphide.
  • soluble tartrate such as sodium potassium tartrate or tartaric acid or ethylene diamine retraacetic acid (referred to hereinafter as EDTA)
  • citric acid or soluble citrates present in sufficient quantity to complex at least a portion of the vanadate, in order to maintain the solubility of the vanadate in the presence of hydrosulphide.
  • the precipitated sulphur may be removed, e.g. by filtration, either before or after the regeneration of the solution.
  • the portion After acidification of the portion of oxidised liquor, the portion is returned to the main liquor stream.
  • the portion will contain all the original components of the Stretford liquor, elemental sulphur, sulphuric acid, sulphate and thionates.
  • the pH of the portion is acid, when admixed back into the main stream, the overall pH will not drop.
  • a further portion of this main stream is now taken and subjected to a sulphur removal step.
  • the sulphur present in the stream is solid elemental sulphur suspended in the liquid phase.
  • This sulphur may be removed either by a physical removal technique such as filtration or by chemical techniques to solubilise the sulphur in the aquesous phase of the liquor.
  • the sulphur may be solubilised for example by heating the oxide stream to between 85 C and boiling.
  • the solubilising reaction is effected in a delay tank and the residence time may be from 2 to 5 hours. At the end of the solubilising step, all the liquor components are in the aqueous phase.
  • This aqueous phase may then be subjected to a solubility lowering technique, for example as described above.
  • the precipitated sulphate may then be removed for example by filtration and the mother liquor returned to the main process stream.
  • the thionates present in the liquor may be destroyed by contacting the liquor with hydrogen sulphide, i.e. when the liquor is reused for the hydrogen sulphide purification step.
  • coal and other fuel gases, effluent air streams, liquid hydrocarbons and other materials can be purified so as to be free from hydrogen sulphide, as shown by the following examples.
  • the pH of the filtrate was brought back to pH 9 by the addition of 5gm/1 Na 2 CO 3 and 25gm/1 Na HCO,.
  • the liquor was then loaded with hydrogen sulphide gas to the level of 0.21 gm/1 and stood for 25 minutes.
  • the concentrations of sodium tetrathionate present in the liquor priot to H 2 S introduction and after the 25 minutes standing period were determined. It was found that the thionate level before H 2 S addition was 1.48 gm/1 and that the end of the standing period the level had dropped to 0.30 gm/l.
  • Example II The procedure of Example II was repeated except that after the expiration of the 210 minute acidification step, the liquor was added to about 5 volumes of a Stretford Liquor which had not undergone acidification.
  • the ADA concentration of the mixed solution was 3gm/l and the suspended elemental sulphur amounted to 1.42gm/l.
  • the amount of sulphur solubilised was determined by difference from the original suspended sulphur, by filtering and weighing.
  • the acid was added via a funnel to the bottom of the reaction vessel.
  • the quantity of SO 2 evolved with time was estimated by arranging that the gaseous effluate should pass through awash bottle wherein any SO 2 was oxidised to the equivalent amount of sulphuric acid hy hydorgen peroxide.
  • the sulphuric acid so produced being continuously titrated (to neutrality) with caustic soda.
  • the quantities of caustic soda used were proportioned to the amounts of SO 2 evolved, these quantities expressed as gms evolved per mole of thiosulphate are shown in curve I of the accompanying drawing.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Removal Of Specific Substances (AREA)
  • Treating Waste Gases (AREA)
EP78300471A 1977-10-13 1978-10-09 Régénération d'une solution absorbante Expired EP0002880B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB4264777 1977-10-13
GB4264777 1977-10-13

Publications (3)

Publication Number Publication Date
EP0002880A2 true EP0002880A2 (fr) 1979-07-11
EP0002880A3 EP0002880A3 (en) 1979-07-25
EP0002880B1 EP0002880B1 (fr) 1982-04-21

Family

ID=10425356

Family Applications (1)

Application Number Title Priority Date Filing Date
EP78300471A Expired EP0002880B1 (fr) 1977-10-13 1978-10-09 Régénération d'une solution absorbante

Country Status (7)

Country Link
US (1) US4360508A (fr)
EP (1) EP0002880B1 (fr)
JP (1) JPS5464072A (fr)
CA (1) CA1112423A (fr)
DE (1) DE2861757D1 (fr)
IT (1) IT1160858B (fr)
ZA (1) ZA785784B (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0074278A1 (fr) * 1981-09-08 1983-03-16 The Dow Chemical Company Traitement de solutions de Stretford contaminées pendant la purification de gaz
EP0097303A1 (fr) * 1982-06-21 1984-01-04 The Dow Chemical Company Elimination d'hydrogène sulfuré de courants fluides avec production minimum de solides
GB2155453A (en) * 1984-03-12 1985-09-25 British Gas Corp Treatment of "Stretford" redox solutions

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI75329C (fi) * 1986-10-22 1988-06-09 Outokumpu Oy Foerfarande foer avlaegsnande av svavelinnehaollet i en uttunnad svaveldioxidhaltig gas.
US4883601A (en) * 1988-08-30 1989-11-28 Union Oil Company Of California Process for purifying an aqueous, hydrogen sulfide-scrubbing solution
US5380442A (en) * 1993-11-18 1995-01-10 Mobil Oil Corporation Regeneration of used stretford solution for recycle
US6180080B1 (en) * 1997-05-14 2001-01-30 Degussa Corporation Removal of thiosulfate from Stretford solution with hydrogen peroxide
US6558646B1 (en) 2000-08-30 2003-05-06 Tosco Corporation Method for increasing the lifetime of stretford solution
US8133399B2 (en) * 2010-06-08 2012-03-13 Conocophillips Company Thiosulfate removal methods and systems

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1102911A (en) * 1913-06-30 1914-07-07 Farbenfab Vorm Bayer F & Co Process of producing sulfur and sulfates.
BE335315A (fr) * 1925-08-06
GB394646A (en) * 1931-01-27 1933-06-29 Metallgesellschaft Ag Process for the production of alkali sulphates and sulphur
DE587653C (de) * 1931-02-12 1933-11-07 Koppers Company Of Delaware Verfahren zur Behandlung der Waschloesungen von Gasreinigungsverfahren
US2046880A (en) * 1933-08-28 1936-07-07 Royal Miller Colloidal sulphur and process of producing the same
DE680675C (de) * 1937-07-06 1939-09-06 I G Farbenindustrie Akt Ges Verfahren zur Reinigung von Gaswaschfluessigkeiten
DE1054648B (de) * 1956-10-24 1959-04-09 Pintsch Bamag Ag Verfahren zum Regenerieren von alkalischen Waschloesungen
US3584042A (en) * 1969-11-24 1971-06-08 Consolidation Coal Co Conversion of thiosulfate to formate
US3644087A (en) * 1970-02-09 1972-02-22 Universal Oil Prod Co Process for scrubbing sulfur dioxide from a gas stream
US3574097A (en) * 1970-02-09 1971-04-06 Universal Oil Prod Co Treating a water stream containing a water-soluble sulfite compound
US3635820A (en) * 1970-08-31 1972-01-18 Universal Oil Prod Co Treating a water stream containing a water-soluble sulfite compound
US3714338A (en) * 1970-12-18 1973-01-30 Universal Oil Prod Co Treating a water stream containing a sulfite compound to produce elemental sulfur
FR2142780B1 (fr) * 1971-06-24 1973-06-29 Inst Francais Du Petrole
GB1448558A (en) * 1972-11-10 1976-09-08 British Gas Corp Gas pruification liquors
GB1434029A (en) * 1972-12-22 1976-04-28 Woodall Duckham Ltd Gas purification
GB1533384A (en) * 1974-11-28 1978-11-22 British Gas Corp Treatment of effluents
US3959452A (en) * 1975-05-15 1976-05-25 Mobil Oil Corporation Process for removing hydrogen sulfide from contaminated gas
DE2623057A1 (de) * 1975-05-27 1976-12-09 Continental Oil Co Regenerierverfahren und vorrichtung zum entfernen von so tief 2 aus einem so tief 2-haltigen gas
US4008310A (en) * 1975-05-27 1977-02-15 Continental Oil Company Regenerative sulfur dioxide scrubbing system
DE2623059A1 (de) * 1975-05-27 1976-12-09 Continental Oil Co Verfahren zum reduzieren einer waessrigen thiosulfat-loesung
US4122148A (en) * 1976-04-20 1978-10-24 Davy Powergas Inc. Sulfur dioxide removal process
US4083945A (en) * 1977-01-10 1978-04-11 Union Oil Company Of California Process for the treatment of hydrogen sulfide gas streams

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0074278A1 (fr) * 1981-09-08 1983-03-16 The Dow Chemical Company Traitement de solutions de Stretford contaminées pendant la purification de gaz
EP0097303A1 (fr) * 1982-06-21 1984-01-04 The Dow Chemical Company Elimination d'hydrogène sulfuré de courants fluides avec production minimum de solides
GB2123395A (en) * 1982-06-21 1984-02-01 Dow Chemical Co Removal of hydrogen sulfide from fluid streams with minimum production of solids
GB2155453A (en) * 1984-03-12 1985-09-25 British Gas Corp Treatment of "Stretford" redox solutions

Also Published As

Publication number Publication date
EP0002880A3 (en) 1979-07-25
IT1160858B (it) 1987-03-11
DE2861757D1 (en) 1982-06-03
JPS5464072A (en) 1979-05-23
EP0002880B1 (fr) 1982-04-21
CA1112423A (fr) 1981-11-17
ZA785784B (en) 1979-09-26
US4360508A (en) 1982-11-23
IT7869364A0 (it) 1978-10-13

Similar Documents

Publication Publication Date Title
US4298584A (en) Removing carbon oxysulfide from gas streams
US4076621A (en) Chelate oxidation of hydrogen sulfide in sour water
JP2637898B2 (ja) 水可溶性無機硫化物を含む水性流を相当する硫酸塩に選択的に製造する方法
RU2241527C2 (ru) Способ десульфуризации газов
US3029201A (en) Water treatment
US4968622A (en) Procedure for microbiologica transformation of sulphur containing harmful components in exhaust gases
EP0221689B1 (fr) Procédé pour le traitement de déchets
US4163043A (en) Process for removing H2 S and CO2 from gases and regenerating the adsorbing solution
GB1563512A (en) Process for separating acid gas and ammonia from dilute aqueous solutions thereof
AU2010224320A1 (en) Process for conversion of waste fluid streams from chemical processing plants to beneficiary agriculture products
US4360508A (en) Treatment of effluents
US3728439A (en) Treatment of a sulfite containing aqueous steam to selectively produce elemental sulfur
US3953577A (en) Process for purifying gases containing HCN
US4017594A (en) Reducing the consumption of anthraquinone disulfonate in Stretford solutions using thiocyanate ion precursors
RU2146693C1 (ru) Способ очистки нефти и/или газоконденсата от сероводорода
RU2019271C1 (ru) Способ очистки пирогаза от диоксида углерода и сероводорода
US5215728A (en) Method and apparatus for removal of h2s from a process gas, including thiosulfate and/or cyanide salt decomposition
US3574097A (en) Treating a water stream containing a water-soluble sulfite compound
EP1265692B1 (fr) Procede de purification de solutions tampons aqueuses
US1401937A (en) Purification of maleic acid by reducing agents
US3714338A (en) Treating a water stream containing a sulfite compound to produce elemental sulfur
NO793188L (no) Fremgangsmaate for aa fjerne hydrogensulfid fra gass-stroemmer
FI75329C (fi) Foerfarande foer avlaegsnande av svavelinnehaollet i en uttunnad svaveldioxidhaltig gas.
US1160375A (en) Process of removing sulfureted hydrogen from gases.
US3690824A (en) Desulfurization of flue gas

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Designated state(s): BE CH DE FR GB NL

AK Designated contracting states

Designated state(s): BE CH DE FR GB NL

17P Request for examination filed
GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): BE CH DE FR GB NL

REF Corresponds to:

Ref document number: 2861757

Country of ref document: DE

Date of ref document: 19820603

NLS Nl: assignments of ep-patents

Owner name: BRITISH GAS PLC TE LONDEN, GROOT-BRITTANNIE.

REG Reference to a national code

Ref country code: FR

Ref legal event code: TP

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19970910

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19970916

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19970918

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19970922

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19970923

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19971002

Year of fee payment: 20

BE20 Be: patent expired

Free format text: 19981009 *BRITISH GAS P.L.C.

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 19981008

Ref country code: CH

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 19981008

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 19981009

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Effective date: 19981008

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

NLV7 Nl: ceased due to reaching the maximum lifetime of a patent

Effective date: 19981009

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT